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DE4126945A1 - METHOD FOR AIR DISASSEMBLY BY RECTIFICATION - Google Patents

METHOD FOR AIR DISASSEMBLY BY RECTIFICATION

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Publication number
DE4126945A1
DE4126945A1 DE4126945A DE4126945A DE4126945A1 DE 4126945 A1 DE4126945 A1 DE 4126945A1 DE 4126945 A DE4126945 A DE 4126945A DE 4126945 A DE4126945 A DE 4126945A DE 4126945 A1 DE4126945 A1 DE 4126945A1
Authority
DE
Germany
Prior art keywords
column
crude argon
argon
oxygen
stream
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
DE4126945A
Other languages
German (de)
Inventor
Dietrich Dipl Ing Rottmann
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Linde GmbH
Original Assignee
Linde GmbH
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Linde GmbH filed Critical Linde GmbH
Priority to DE4126945A priority Critical patent/DE4126945A1/en
Priority to JP4253394A priority patent/JPH05203348A/en
Priority to CA002075737A priority patent/CA2075737A1/en
Priority to EP92113843A priority patent/EP0527501A1/en
Priority to ZA926089A priority patent/ZA926089B/en
Priority to AU20993/92A priority patent/AU2099392A/en
Priority to CN92109305A priority patent/CN1069329A/en
Priority to US07/929,180 priority patent/US5251449A/en
Publication of DE4126945A1 publication Critical patent/DE4126945A1/en
Withdrawn legal-status Critical Current

Links

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/04103—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression using solely hydrostatic liquid head
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
    • F25J3/04206—Division of the main heat exchange line in consecutive sections having different functions including a so-called "auxiliary vaporiser" for vaporising and producing a gaseous product
    • F25J3/04212—Division of the main heat exchange line in consecutive sections having different functions including a so-called "auxiliary vaporiser" for vaporising and producing a gaseous product and simultaneously condensing vapor from a column serving as reflux within the or another column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04327—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of argon or argon enriched stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04351—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04369—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of argon or argon enriched stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04654—Producing crude argon in a crude argon column
    • F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04654—Producing crude argon in a crude argon column
    • F25J3/04709—Producing crude argon in a crude argon column as an auxiliary column system in at least a dual pressure main column system
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/20—Processes or apparatus using separation by rectification in an elevated pressure multiple column system wherein the lowest pressure column is at a pressure well above the minimum pressure needed to overcome pressure drop to reject the products to atmosphere
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
    • F25J2200/52—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column in the high pressure column of a double pressure main column system
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/58—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being argon or crude argon
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/50—Processes or apparatus involving steps for recycling of process streams the recycled stream being oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/20—Boiler-condenser with multiple exchanger cores in parallel or with multiple re-boiling or condensing streams
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/50—One fluid being oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/58—One fluid being argon or crude argon
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S62/00—Refrigeration
    • Y10S62/923—Inert gas
    • Y10S62/924—Argon

Landscapes

  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Health & Medical Sciences (AREA)
  • Emergency Medicine (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Description

Gegenstand der Erfindung ist ein Verfahren zur Luftzerlegung durch Rektifikation, bei dem Luft verdichtet, vorgereinigt, abgekühlt und in der Hochdrucksäule einer zweistufigen Rektifikationssäule in eine sauerstoffreiche Flüssigkeit und in eine stickstoffreiche Fraktion vorzerlegt wird, die sauer­ stoffreiche Flüssigkeit vollständlg und die stickstoffreiche Fraktion mindestens teilweise der Mitteldrucksäule der Rektifikationssäule zugeführt und in Sauerstoff und Stickstoff zerlegt wird und bei dem der Mitteldrucksäule ein argonhaltiger Sauerstoffstrom und ein flüssiger Sauerstoff-Produktstrom entnommen werden, wobei der argonhaltige Sauerstoffstrom einer Rohargonsäule, die bei einem Druck betrieben wird, der niedriger als der Druck der Mitteldrucksäule ist und aus deren oberem Bereich Rohargon entnommen wird, zugeleitet wird.The invention relates to a method for air separation by rectification, in which air is compressed, pre-cleaned, cooled and in the high-pressure column of a two-stage Rectification column into an oxygen-rich liquid and a nitrogen-rich fraction is pre-decomposed, which is acidic complete substance-rich liquid and the nitrogen-rich Fraction at least partially of the medium pressure column of the Rectification column fed and in oxygen and nitrogen is disassembled and in which the medium pressure column contains an argon Oxygen stream and a liquid oxygen product stream are taken, the argon-containing oxygen flow one Raw argon column, which is operated at a pressure that is lower than and from the pressure in the medium pressure column the upper area is taken from raw argon, is fed.

Ein derartiges Verfahren, bei dem im Anschluß an eine Luft­ zerlegung Rohargon gewonnen wird, ist aus der DE-OS 39 05 521 bekannt. Such a method in which following an air decomposition crude argon is obtained from DE-OS 39 05 521 known.  

Bei diesem Verfahren wird die Rohargonrektifikation bei einem Druck durchgeführt, der niedriger ist als der Druck, bei dem die Mitteldrucksäule der zweistufigen Rektifikationssäule betrieben wird. Der argonhaltige Sauerstoffstrom aus der Mitteldrucksäule wird vor dem Einleiten in die Rohargonsäule arbeitsleistend entspannt und vermag auf diese Weise die ganze oder zumindest einen großen Teil der benötigten Prozeßkälte zu liefern. Am Sumpf der Hochdrucksäule wird eine sauerstoffreiche Flüssigkeit abgezogen, die zum größten Teil dazu verwendet wird, im Kopfkondensator der Rohargonsäule gasförmiges Rohargon teilweise zu verflüssigen.In this procedure, the crude argon rectification is carried out at a Pressure carried out that is lower than the pressure at which the medium pressure column of the two-stage rectification column is operated. The argon-containing oxygen flow from the Medium pressure column is before the introduction into the crude argon column Relaxes while working and can do the whole thing or at least a large part of the required process cooling deliver. At the bottom of the high pressure column there is an oxygen-rich one Withdrawn liquid, which is used for the most part gaseous crude argon in the top condenser of the crude argon column partially liquefy.

Damit der in diesem Strom enthaltenen Sauerstoff zurückgewonnen werden kann, wird er zur Mitteldrucksäule zurückgeführt. Um den dafür notwendigen Druck zu erreichen, wird der sauerstoffreiche Strom vor dem Einspeisen in die Mitteldrucksäule in zwei Verdichterstufen komprimiert und jeweils anschließend abgekühlt.So that the oxygen contained in this stream is recovered can be returned to the medium pressure column. To the to reach the necessary pressure, the oxygen-rich Electricity before feeding into the medium pressure column in two Compressor stages compressed and then cooled each time.

Bei dem bekannten Verfahren erweist sich jedoch ein Merkmal als nachteilig. Die in der Rohargonsäule angewandte Kopfkühlung mittels der am Sumpf der Hochdrucksäule der zweistufigen Rektifikationssäule abgezogenen und vor dem Eintritt in den Kopf der Rohargonsäule entspannten sauerstoffreichen Flüssigkeit ist verfahrenstechnisch sehr aufwendig.In the known method, however, a feature proves to be disadvantageous. The head cooling used in the raw argon column by means of the two-stage at the bottom of the high pressure column Rectification column deducted and before entering the Head of the raw argon column relaxed oxygen-rich In terms of process technology, liquid is very complex.

Die Aufgabe, welche der Erfindung zugrunde liegt, besteht darin, ein Verfahren der eingangs genannten Art dahingehend zu verbessern, daß sowohl auf eine verfahrenstechnisch aufwendige Kopfkühlung der Rohargonsäule verzichtet als auch die Argon­ gewinnung wirtschaftlich günstig durchgeführt werden kann.The object on which the invention is based is in that to a method of the type mentioned improve that both on a procedurally complex Head cooling of the raw argon column dispenses with the argon extraction can be carried out economically.

Diese Aufgabe wird dadurch gelöst, daß das entnommene Rohargon zunächst in indirektem Wärmetausch gegen kondensiertes Rohargon und gegen Luft erwärmt wird, anschließend ein erster Teilstrom des Rohargons in indirektem Wärmeaustausch mit dem flüssigen Sauerstoff-Produktstrom kondensiert wird, wobei der Sauerstoff- Produktstrom teilweise verdampft, wonach das kondensierte Rohargon wieder in die Rohargonsäule zurückgeleitet und ein zweiter Teilstrom des Rohargons als Produkt gewonnen wird.This object is achieved in that the raw argon removed initially in indirect heat exchange against condensed raw argon and heated against air, then a first partial flow of raw argon in indirect heat exchange with the liquid  Oxygen product stream is condensed, the oxygen Product stream partially evaporated, after which the condensed Raw argon is fed back into the raw argon column and on second partial stream of raw argon is obtained as a product.

Dadurch lassen sich gegenüber dem bekannten Verfahren mehrere Verbesserungen erzielen. So gelangt nun die gesamte Luft dampfförmig in die Hochdrucksäule, wodurch sich bereits rektifikatorische Vorteile ergeben. Eine Vorverflüssigung in einem Nebenkondensator, wie sie bei dem bekannten Verfahren unter den angegebenen Rektifizierdrücken notwendig werden kann, ist nun nicht mehr notwendig.As a result, several can be compared to the known method Make improvements. So now all the air gets through in vapor form in the high pressure column, which is already rectification benefits. A pre-liquefaction in a secondary capacitor, as in the known method under the specified rectification pressures, is no longer necessary.

Auch wird beim erfindungsgemäßen Verfahren die Rektifikation in der Mitteldrucksäule verbessert, da die, dem Sumpf der Hoch­ drucksäule entnommene, sauerstoffreiche Flüssigkeit vollständig in die Mitteldrucksäule entspannt wird.In the method according to the invention, rectification is also carried out in the medium pressure column improved since that, the swamp of the high All oxygen-rich liquid removed from the pressure column is relaxed in the medium pressure column.

Eine Verbesserung der Rektifikation im unteren Abschnitt der Mitteldrucksäule wird zusätzlich dadurch erreicht, daß die aus dem Sumpf der Rohargonsäule in die Mitteldrucksäule zurückge­ pumpte Flüssigkeit nicht mehr, wie bei dem bekannten Verfahren, ein Bestandteil der Luft ist, sondern als Fremdzuspeisung den Rücklauf auf die Mitteldrucksäule erhöht. Dadurch verschiebt sich das Flüssigkeit-zu-Dampf-Verhältnis F/D in Richtung 1.An improvement in rectification in the lower section of the Medium pressure column is also achieved in that the the bottom of the crude argon column back into the medium pressure column no longer pumped liquid, as in the known method, is a component of the air, but as an external supply Return to the medium pressure column increased. This shifts the liquid-to-vapor ratio F / D towards 1.

Beim erfindungsgemäßen Verfahren erweist es sich als vorteil­ haft, wenn der erste Rohargon-Teilstrom vor dem indirekten Wärmetausch mit dem flüssigen Sauerstoff-Produktstrom verdich­ tet und abgekühlt wird. Hierbei kann das Verdichten und das sich jeweils anschließende Abkühlen in einer oder mehreren Stufen erfolgen.In the method according to the invention, it proves to be advantageous liable if the first crude argon partial stream before the indirect Compress heat exchange with the liquid oxygen product stream tet and cooled. Here, the compression and the each subsequent cooling in one or more Levels.

Mittels des bzw. der Verdichter läßt sich somit der gewünschte Druck des Rohargons und damit letztendlich das Druckniveau des verdampften Sauerstoff-Produktstromes einstellen. The desired compressor can thus be used by means of the compressor or compressors Pressure of the raw argon and ultimately the pressure level of the set vaporized oxygen product flow.  

Eine weitere Ausgestaltung des Erfindungsgedankens ist dadurch gekennzeichnet, daß der kondensierte erste Rohargon-Teilstrom vor dem Zurückleiten in die Rohargonsäule im indirekten Wärmetausch gegen aus der Rohargonsäule entnommenes Rohargon weiter abgekühlt und entspannt wird.A further embodiment of the inventive concept is thereby characterized in that the condensed first crude argon substream before returning to the raw argon column in the indirect Heat exchange for raw argon taken from the raw argon column is further cooled and relaxed.

Als besonders vorteilhaft erweist es sich, wenn der Druck des flüssigen Sauerstoff-Produktstromes mittels einer Pumpe erhöht wird, bevor der flüssige Sauerstoff-Produktstrom in den Konden­ satorverdampfer geführt wird.It proves to be particularly advantageous if the pressure of the liquid oxygen product stream increased by means of a pump is before the liquid oxygen product stream in the condensers sator evaporator is performed.

Eine weitere vorteilhafte Ausgestaltung ist dadurch gekenn­ zeichnet, daß ein Teil des verdampften Sauerstoff-Produktstromes in den unteren Teil der Mitteldrucksäule entspannt wird.A further advantageous embodiment is characterized records that part of the vaporized oxygen product stream is relaxed in the lower part of the medium pressure column.

Mittels dieser beiden letzten Ausführungsformen ist ein genaues Einstellen der gewünschten Sauerstoff-Produktstrommenge in der aus der Anlage zum Kunden bzw. Verbraucher führenden Leitung möglich.By means of these last two embodiments is an exact one Set the desired amount of oxygen product flow in the from the plant to the customer or consumer leading line possible.

Anhand der Zeichnung, in welcher eine Ausführungsform des erfindungsgemäßen Verfahrens schematisch dargestellt ist, werden die Erfindung und weitere Einzelheiten der Erfindung näher erläutert.Based on the drawing, in which an embodiment of the the method according to the invention is shown schematically, become the invention and further details of the invention explained in more detail.

Über Leitung 1 wird verdichtete und vorgereinigte Luft herange­ führt, in einem Wärmetauscher 36 im indirekten Wärmeaustausch mit Produktströmen abgekühlt und in die Hochdrucksäule 3 einer zweistufigen Rektifiziersäule 2 eingespeist. Die Hochdrucksäule 3 (Betriebsdruck: 6 bis 20 bar, vorzugsweise 8 bis 17 bar) steht mit der Mitteldrucksäule 4 (Betriebsdruck: 1,5 bis 10 bar, vorzugsweise 2,0 bis 8 bar) über einen gemeinsamen Kondensator/ Verdampfer 13 in wärmetauschender Verbindung. Die eingeführte Luft wird in der Hochdrucksäule in Stickstoff und in eine sauerstoffangereicherte Fraktion vorzerlegt. Die sauerstoff­ angereicherte Fraktion wird am Sumpf der Hochdrucksäule über Leitung 6 in flüssigem Zustand abgeführt, in Wärmetauscher 32 unterkühlt und über Ventil 10 wieder in die Mitteldrucksäule 4 eingedrosselt. Stickstoff vom Kopf der Hochdrucksäule 3 wird über Leitung 5 ebenfalls flüssig abgezogen, in Wärmetauscher 32 unterkühlt und zum einen über Leitung 8 als flüssiges Produkt abgeführt. Der andere Teil des Stickstoffs aus der Drucksäule 3 wird über Leitung 9 als Rücklauf auf die Mitteldrucksäule 4 gegeben.Compressed and pre-cleaned air is supplied via line 1 , cooled in a heat exchanger 36 in indirect heat exchange with product streams, and fed into the high-pressure column 3 of a two-stage rectification column 2 . The high pressure column 3 (operating pressure: 6 to 20 bar, preferably 8 to 17 bar) is connected to the medium pressure column 4 (operating pressure: 1.5 to 10 bar, preferably 2.0 to 8 bar) via a common condenser / evaporator 13 . The air introduced is pre-divided in the high pressure column into nitrogen and into an oxygen-enriched fraction. The oxygen-enriched fraction is discharged in the liquid state at the bottom of the high-pressure column via line 6 , subcooled in heat exchanger 32 and throttled back into the medium-pressure column 4 via valve 10 . Nitrogen from the top of the high-pressure column 3 is also drawn off in liquid form via line 5 , supercooled in heat exchanger 32 and, on the one hand, discharged as a liquid product via line 8 . The other part of the nitrogen from the pressure column 3 is fed via line 9 as a return to the medium pressure column 4 .

Als Produkte der Mitteldruckstufe werden flüssiger Sauerstoff (Leitung 40), gasförmiger Reinstickstoff (Leitung 15) und unreiner Stickstoff (Leitung 16) entnommen und die beiden Stickstoff-Fraktionen in den Wärmetauschern 32 und 36 angewärmt.Liquid oxygen (line 40 ), gaseous pure nitrogen (line 15 ) and impure nitrogen (line 16 ) are removed as products of the medium pressure stage and the two nitrogen fractions in the heat exchangers 32 and 36 are heated.

Sollte die Kälteleistung der Turbine 18 nicht für den Prozeß ausreichen, so ist es zweckmäßig, wegen des relativ hohen Druckes in der Mitteldrucksäule 4 den unreinen Stickstoff in Leitung 16 zur Erzeugung von fehlender Verfahrenskälte zu verwenden. Die dazu nötigen Verfahrensschritte sind in der Zeichnung jedoch nicht dargestellt.If the cooling capacity of the turbine 18 is not sufficient for the process, it is expedient to use the impure nitrogen in line 16 because of the relatively high pressure in the medium-pressure column 4 in order to generate no process cold. The necessary process steps are not shown in the drawing.

Über die bisher genannten Ströme hinaus wird der Mitteldruck­ säule 4 außerdem ein argonhaltiger Sauerstoffstrom über Leitung 17 entnommen, im Wärmetauscher 36 angewärmt und in die Rohar­ gonsäule 20 eingespeist, die unter einem Druck von 1,1 bis 2 bar, vorzugsweise 1,3 bis 1,5 bar betrieben wird. Die im Sumpf der Rohargonsäule 20 anfallende Restfraktion wird über Leitung 22 abgeführt und durch Pumpe 23 auf den für die Zurückspeisung in die Mitteldrucksäule 4 erforderlichen Druck gebracht. Ferner wird der argonreiche Sauerstoffstrom 17 vor dem Einleiten in die Rohargonsäule 20 in einer Entspannungsturbine 18 arbeits­ leistend entspannt, um den argonreichen Sauerstoffstrom einer­ seits auf den in der Rohargonsäule 20 herrschenden niedrigen Druck zu bringen und andererseits benötigte Verfahrenskälte zu erzeugen. In addition to the currents mentioned above, the medium-pressure column 4 is also an argon-containing oxygen stream removed via line 17 , warmed in the heat exchanger 36 and fed into the Rohar gonsäule 20 , which under a pressure of 1.1 to 2 bar, preferably 1.3 to 1 , 5 bar is operated. The residual fraction obtained in the bottom of the crude argon column 20 is discharged via line 22 and brought to the pressure required for feeding back into the medium pressure column 4 by pump 23 . Furthermore, the argon-rich oxygen stream 17 is relaxed before it is introduced into the crude argon column 20 in an expansion turbine 18 , in order to bring the argon-rich oxygen stream on the one hand to the low pressure prevailing in the crude argon column 20 and, on the other hand, to produce the required process cold.

Das am Kopf der Rohargonsäule 20 anfallende gasförmige Rohargon wird über Leitung 21 entnommen, im Wärmetauscher 37 gegen abkühlendes, kondensiertes Rohargon erwärmt, desweiteren im Wärmetauscher 36 erwärmt und daran anschließend in zwei Teil­ ströme 24 und 25 aufgeteilt. Der Rohargonstrom in Leitung 24 wird als Zwischenprodukt aus der Anlage zum Verbraucher abgeführt. Der nicht aus der Anlage abgeführte Rohargonstrom in Leitung 25 wird in zwei Verdichterstufen 26 und 29 komprimiert und jeweils anschließend abgekühlt (Wasserkühler 28 und 30). Anschließend wird der Rohargonstrom über Leitung 31 durch den Wärmetauscher 36 geführt, dort weiter abgekühlt und daran anschließend in den, im Kondensatorverdampfer 33 angebrachten Kondensator 34 geführt. Im Kondensator 34 kondensiert das Rohargon gegen über Leitung 40 und mit Hilfe von Pumpe 41 herangeführten, flüssigen Sauerstoff. Das kondensierte Rohargon wird anschließend über Leitung 35 in den Wärmetauscher 37 geführt, in ihm gegen aus der Rohargonsäule 20 entnommenes Rohargon abgekühlt und über Ventil 38 in die Rohargonsäule 20 entspannt.The resulting at the top of the crude argon column 20 gaseous crude argon is removed via line 21 , heated in the heat exchanger 37 against cooling, condensed crude argon, further heated in the heat exchanger 36 and then divided into two partial streams 24 and 25 . The crude argon stream in line 24 is removed as an intermediate product from the system to the consumer. The crude argon stream in line 25 , which is not removed from the system, is compressed in two compressor stages 26 and 29 and then each cooled (water coolers 28 and 30 ). The crude argon stream is then passed through line 31 through the heat exchanger 36 , further cooled there, and then subsequently led into the condenser 34 installed in the condenser evaporator 33 . In the condenser 34, the crude argon condenses against liquid oxygen brought in via line 40 and by means of pump 41 . The condensed crude argon is then fed via line 35 into the heat exchanger 37 , cooled in it against crude argon taken from the crude argon column 20 and expanded into the crude argon column 20 via valve 38 .

Der über Leitung 40 und mit Hilfe der Pumpe 41 in den Konden­ satorverdampfer 33 geführte, flüssige, unter Druck stehende Sauerstoff-Produktstrom wird im indirekten Wärmetausch mit dem Teilstrom des über Leitung 31 herangeführten Rohargons teilweise verdampft. Die dampfförmige Fraktion des Sauerstoff-Produkt­ stromes wird über Leitung 42 nach Erwärmen im Wärmetauscher 36 abgegeben. Über Leitung 43 und Ventil 44 kann ein nicht zur Abgabe benötigter Teil des gasförmigen Sauerstoff-Produkt­ stromes wieder in den Sumpf der Mitteldrucksäule entspannt werden. Mittels Leitung 45 läßt sich ein flüssiger Sauerstoff- Produktstrom aus dem Kondensatorverdampfer 33 gewinnen.The conducted via line 40 and with the help of the pump 41 in the condenser capacitor 33 , liquid, pressurized oxygen product stream is partially evaporated in indirect heat exchange with the partial stream of the raw argon introduced via line 31 . The vaporous fraction of the oxygen product stream is discharged via line 42 after heating in the heat exchanger 36 . Via line 43 and valve 44 , a part of the gaseous oxygen product stream not required for delivery can be expanded again into the sump of the medium pressure column. A liquid oxygen product stream can be obtained from the condenser evaporator 33 by means of line 45 .

Die in der Zeichnung gestrichelt gezeichneten Verfahrens­ schritte stellen einen zusätzlichen Stickstoff-Verstärkungs­ kreislauf dar. The procedure drawn in dashed lines in the drawing steps provide an additional nitrogen boost cycle.  

Über Leitung 50 wird ein Teil der Stickstofffraktion aus Lei­ tung 15 entnommen, im Verdichter 51 komprimiert, anschließend im Wasserkühler 52 abgekühlt und über Leitung 53 nach unterküh­ len in Wärmetauscher 36 in die, im Sumpf der Hockdrucksäule 3 angebrachten Heizschlange 54 geführt. Das so gebildete Stick­ stoffkondensat wird über Leitung 55 und Ventil 56 in den oberen Bereich der Hochdrucksäule, ober- oder unterhalb der Entnahme­ stelle des flüssigen Stickstoffs (Leitung 5) eingeführt (in der Zeichnung ist der Übersichtlichkeit halber die Einführung unter­ halb der Entnahmestelle gezeichnet). Das im oberen Bereich der Hochdrucksäule eingedrosselte Stickstoffkondensat wirkt sich in der Mitteldrucksäule positiv für die Argongewinnung aus, da die Rücklaufverhältnisse in der Mitteldrucksäule durch die zusätz­ liche Stickstoff-Aufgabe verbessert werden.Part 50 of the nitrogen fraction is taken from line 15 via line 50 , compressed in the compressor 51 , then cooled in the water cooler 52 and passed via line 53 to subcooling in heat exchanger 36 into the heating coil 54 attached in the sump of the high pressure column 3 . The thus formed nitrogen condensate is introduced via line 55 and valve 56 into the upper area of the high-pressure column, above or below the point of withdrawal of the liquid nitrogen (line 5 ) (in the drawing, the introduction below half the point of withdrawal is drawn for the sake of clarity) . The nitrogen condensate throttled in the upper area of the high pressure column has a positive effect on argon production in the medium pressure column, since the reflux conditions in the medium pressure column are improved by the additional nitrogen task.

Ferner läßt sich durch die Sumpfheizung 54 die benötigte Luftmenge so weit reduzieren, daß jede beliebig niedrige Sauerstoffreinheit im unreinen Stickstoff realisierbar ist.Furthermore, the sump heater 54 allows the amount of air required to be reduced to such an extent that any low level of oxygen purity in impure nitrogen can be achieved.

Claims (6)

1. Verfahren zur Luftzerlegung durch Rektifikation, bei dem Luft (1) verdichtet, vorgereinigt, abgekühlt (36) und in der Hochdrucksäule (3) einer zweistufigen Rektifikations­ säule (2) in eine sauerstoffreiche Flüssigkeit (6) und in eine stickstoffreiche Fraktion (5) vorzerlegt wird, die sauerstoffreiche Flüssigkeit (6) vollständig und die stickstoffreiche Fraktion (5) mindestens teilweise der Mitteldrucksäule (4) der Rektifikationssäule (2) zugeführt und in Sauerstoff und Stickstoff zerlegt wird und bei dem der Mitteldrucksäule (4) ein argonhaltiger Sauerstoffstrom (17) und ein flüssiger Sauerstoff-Produktstrom (40) entnommen werden, wobei der argonhaltige Sauerstoffstrom einer Rohargonsäule (20), die bei einem Druck betrieben wird, der niedriger als der Druck der Mitteldrucksäule (4) ist und aus deren oberem Bereich Rohargon (21) entnommen wird, zugeleitet wird, dadurch gekennzeichnet, daß das entnommene Rohargon zunächst in indirektem Wärmetausch gegen kondensiertes Rohargon (35) und gegen Luft (1) erwärmt wird (37, 36), anschließend ein erster Teilstrom des Rohargons (25, 31) in indirektem Wärmeaustausch (34) mit dem flüssigen Sauerstoff-Produktstrom (40) kondensiert (35) wird, wobei der Sauerstoff-Produktstrom (40) teilweise verdampft, wonach das kondensierte Rohargon (35) wieder in die Rohargonsäule (20) zurückgeleitet und ein zweiter Teilstrom des Rohargons als Produkt (24) gewonnen wird. 1.A method for air separation by rectification, in which air ( 1 ) is compressed, pre-cleaned, cooled ( 36 ) and in the high-pressure column ( 3 ) a two-stage rectification column ( 2 ) into an oxygen-rich liquid ( 6 ) and into a nitrogen-rich fraction ( 5 ) is disassembled, the oxygen-rich liquid ( 6 ) completely and the nitrogen-rich fraction ( 5 ) at least partially fed to the medium pressure column ( 4 ) of the rectification column ( 2 ) and broken down into oxygen and nitrogen and in which the medium pressure column ( 4 ) contains an argon-containing oxygen stream ( 17 ) and a liquid oxygen product stream ( 40 ) are taken, the argon-containing oxygen stream of a crude argon column ( 20 ), which is operated at a pressure which is lower than the pressure of the medium pressure column ( 4 ), and crude argon ( 21 is removed) is fed, characterized in that the removed crude argon, first in indirect W rmetausch against condensed crude argon (35) and against air (1) is heated (37, 36), then a first partial stream of the crude argon (25, 31) condensed in indirect heat exchange (34) with the liquid oxygen product stream (40) (35 ), the oxygen product stream ( 40 ) partially evaporating, after which the condensed crude argon ( 35 ) is returned to the crude argon column ( 20 ) and a second partial stream of crude argon is obtained as product ( 24 ). 2. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß der erste Rohargon-Teilstrom (25) vor dem indirekten Wärme­ tausch (34) verdichtet (26, 29) und abgekühlt (28, 30, 36) wird.2. The method according to claim 1, characterized in that the first crude argon partial stream ( 25 ) before the indirect heat exchange ( 34 ) compressed ( 26 , 29 ) and cooled ( 28 , 30 , 36 ). 3. Verfahren nach Anspruch 1 und 2, dadurch gekennzeichnet, daß das Verdichten und Abkühlen des ersten Rohargon- Teilstromes in einer oder mehreren Stufen erfolgt.3. The method according to claim 1 and 2, characterized in that the compression and cooling of the first raw argon Partial flow takes place in one or more stages. 4. Verfahren nach einem der Ansprüche 1 bis 3, dadurch gekenn­ zeichnet, daß der kondensierte erste Rohargon-Teilstrom (35) vor dem Zurückleiten in die Rohargonsäule in indirektem Wärmetausch gegen aus der Rohargonsäule entnommenes Rohargon (21) weiter abgekühlt (37) und entspannt (38) wird.4. The method according to any one of claims 1 to 3, characterized in that the condensed first crude argon partial stream ( 35 ) further cooled ( 37 ) and relaxed before returning to the crude argon column in indirect heat exchange against crude argon ( 21 ) taken from the crude argon column ( 38 ) will. 5. Verfahren nach einem der Ansprüche 1 bis 4, dadurch gekenn­ zeichnet, daß der Druck des flüssigen Sauerstoff-Produkt­ stromes (40) mittels einer Pumpe (41) erhöht wird, bevor der flüssige Sauerstoff-Produktstrom in den Kondensator­ verdampfer (33) geführt wird.5. The method according to any one of claims 1 to 4, characterized in that the pressure of the liquid oxygen product stream ( 40 ) by means of a pump ( 41 ) is increased before the liquid oxygen product stream in the condenser evaporator ( 33 ) becomes. 6. Verfahren nach einem der Ansprüche 1 bis 5, dadurch gekenn­ zeichnet, daß ein Teil des verdampften Sauerstoff-Produkt­ stromes (44) in den unteren Teil der Mitteldruckstufe entspannt wird (45).6. The method according to any one of claims 1 to 5, characterized in that a part of the vaporized oxygen product stream ( 44 ) is relaxed ( 45 ) in the lower part of the medium pressure stage.
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JP4253394A JPH05203348A (en) 1991-08-14 1992-08-10 Air separation by refining and its apparatus
CA002075737A CA2075737A1 (en) 1991-08-14 1992-08-11 Process and apparatus for air fractionation by rectification
EP92113843A EP0527501A1 (en) 1991-08-14 1992-08-13 Air rectification process and apparatus
ZA926089A ZA926089B (en) 1991-08-14 1992-08-13 Process and apparatus for air fractionation by rectification.
AU20993/92A AU2099392A (en) 1991-08-14 1992-08-13 Process and apparatus for air fractionation by rectification
CN92109305A CN1069329A (en) 1991-08-14 1992-08-13 The method and apparatus of seperating air by rectification
US07/929,180 US5251449A (en) 1991-08-14 1992-08-13 Process and apparatus for air fractionation by rectification

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